Process for converting petroleum oil



Original Filed Dec. 1, 1922 #22 fans:

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Patented Dec. 2, 1930 UNITED ATENT OFFICE GUWIPAV EGLOFF JACQUE C. HOB-BELL, CMOAG O ILLINDIS, ASSIGNORS 10 UNT- t' Q. i SQUTE DAKOTA.

'EBOOESS FOR C0 a OIL PRODUCTS comm, OE CMCAGQ, ILLINOIS, A. COBJEORATION 0F mm are anon orn- Applicatien med December 1, 1922, Serial Ito. H'- Renewed February 5, 1929.

This invention relates to improvements in a process and apparatus for converting petrole oil and refers more particularly to the conversion of hydrocarbon products from t oils of a relatively high boiling point to oils of aliower boiling point such as gasoline and the l' e.

'ong the objects of the invention are to provide a process in which after cracking the to oil under pressure and subjecting it to a reduring and condensing action the uncondensed gases are re-treated to extract therefrom light hydrocarbons which may be contained therein, to provide a process in which W these gases are retreated to produce light hydrocarbons in separate stages which may be alternately isolated from the system whereby more continuous operation is eflected. The single figure is a diagrammatic side elevational view of the apparatus.

U ed by means of gas burners The 011 after being circulated therethrough is raised to a conversion temperature and in this condition passes through the transfer line 8 regulated by a valve 9 to the conversion or va rizing chamber 10. This chamber prefera ly consists of an enlarged tank or receptacle which may be heavily insulated to prevent loss of heat by radiation. Try-cocks 11 are tapped in at different levels in order that the operators may ascertain the level of the oil at all times. Separate residuum lines 12 controlled by valves 13 furnish a means for withdrawing unvaporized oil constituents from the vaporizing stage. The evolved vapors and gases rise through the line 14 controlled by a valve 15 and are introduced to the bottom of the dephlegmating or refluxing column 16. The vapors rising through the refluxing column are interrupted by a series of perforated pans 17 in which the condensate separated from the vapors may collect, dropping back to the bottom of the refluxing column and there being collected in the dephlegmator leg 18 and returned to the charging line through the pipe 19 controlled by a valve 2t). H e reflux condensate becomes excesslve, portions may be drawn ofi through a line 21 controlled by a. valve 22 and directed to any convenient storage. The vapors passing ofi from the top of the dephlegmator pass through the line 23 regulated by a valve 24 to the condenser coil 25 ositioned in the water condenser box 26. lhe' liquid distillate condensed therein flows down through the line 27 controlled by a valve 28 and is collected in the receiving tank 29. This latter tank is equipped with a liquid level gauge 30,

pressure gauge 31, a liquid draw-ofi line 32 controlled by a valve 33 and a gas draw-oil line 34 controlled by a valve 35. The liquid draw-0d line 32 communicates with a separating tank '36 to which the liquid distillate 1 is directed and permitted to collect under a lower pressure, which is controlled by the valve 33. The tank is equipped with a liquid level gauge 37, a liquid draw-ofi line 38 regulated by a valve 39 and a gas draw-off line 40 in which is interposed a throttle valve 41. The release in pressure on this tank may be any pressure ranging from a pressure slightly below the pressure maintained upon the system down to atmospheric, or a vacuum pressure may be im osed by means of the vacuum pump 42. ith this lowering of pressure uponthe distillate there is an increased evolution of gaseous vapors which are drawn ofi through the line 40 and directed through the pump 42 into the line 43. This line has communication with the gas line 34 tapped into the top of the receiving tank 29. A by-pass line 44 regulated by a valve 45 furnishes a means for by-passing the gases from the receiving tank to the suction side of the vacuum pump. The gases from the separating tank 36 and receiving tank' 29 are thus charged through the line 43 into either of the columns 46 or 47. These columns are preferably cylindrical in form, having a zone of checker work brick as shown at 48 in their lower portions. Above these bricked portions is a broken up and absorbent agent such as charcoal shown at 49. The columns are connected into the system so that either may be isolated therefrom while the other is being operated as a part of the system, that is, the gases flowing through the pipe 43 may be introduced to the column 46 through the secondary line 50 and perforated rose 51 by opening the valve 52. On the other hand by closing the valve 52 the gases will pass on and may be introduced to the column 47 by opening the valve 53 interposed in the line 54, the upper end of which terminates in a rose 55 identical in construction to that shown at 51 in the column 46. As an alternative and in case both columns are to be cut out of the system, the gases may be directed through the line 56 by closing the valves 52 and 53 and opening the valve 57.

Assuming the column 47 is cut out of the system and the gases are directed into the column 46 under such conditions the valves 53 and 57 will be closed and the valve 52 opened.

The gases containing light hydrocarbon which remained uncondensed after condensation in the water condenser coil. 25 will rise through the checker work brick and percolate through the broken up absorbent agent contained thereabove. The light hydrocarbons separable from these gaseous vapors will be both absorbed and adsorbed while the incondensible gas will pass of from the top of the column through the lines 58 and 59 con-' trolled by valves 60 and 61 respectively to the gasometer 62. When the absorbent agent in the column has become saturated or sub stantially so the valves 52 and 60 may be closed and the valves 53 and 63 opened, the

latter valve 63 being in the upper gas drawofi' line 64 by means of which uncondensed gas from the column. 47 is withdrawn.

In the meantime a portion of the expended combustion gases are withdrawn from the stack 65 and returned through the line 66 controlled by valve 67 to the pump 68 by means of which they are caused to pass through a coil 69 positioned in the furnace 6, thus these gases are heated to a high temperature and directed through the insulated line 7 0 controlled by a valve 71 to the header 72 which is connected to the line by a secondary connection 73 and valve 74 is interposed in this latter line.

After the colunm 46 has been cut out of the system these heated gases are returned and injected into the column through a pipe 75 controlled by a valve 76. The temperature of these gases is suflicient to readily drive off the lighter hydrocarbons which were taken up by the broken fragmentary material shown at 49. These light hydrocarbons in a vaporous condition pass off through the line 77 regulated by a valve 78 and into the pipe 79 communicating with the water condenser coil 80 where they are reduced to liquid form and collected in the receiving tank 81 communicating with the discharge end of the condenser coil. The receiving tank 81 is equipped with a liquid level gauge 82, pressure gauge 83 and liquid draw-ofi' valve 84 and a pressure relief valve 85. If desirable steam may be introduced through the pipe 86 in which is interposed a valve 87. The introduction of steam with certain hydrocarbons has the effect, as is well known in the art, of improving the quality of the distillate.

In a like manner when the column 46 has been cut into the system and the column 47 cut out, the heated gases are directed to the latter column through an injector pipe 86 similar to that shown at 75 connected and to the header 72. The vaporous hydrocarbons driven from the column 47 pass through the line 87 controlled bya valve 88 to the line 79 and thence through the condensing apparatus explained in connection with the column 46.

. Thus the apparatus may be operated continuously and if necessary any number of saturating columns may be connected up with the system. It is a well known fact that in cracking hydrocarbon oil there is a large portion of light hydrocarbon fractions which are lost with the incondensible gases and by separately treating the ases in this manner a substantial portion 0 fractions. may be extracted.

By treating midcontinent gas oil of approximately 32 Baum gravity to temperatures ranging from 700 to 1000 F. and under pressures ranging from 50 to 500 pounds a yield of good quality distillate may be obtained comprising from 50 to 75% of the oil charged. In connection with this conversation a large volume of incondensible gas is formed from which may be extracted a light distillate having gravities upward of 55 Baum gravity.

I claim:

1. A process for cracking oil consisting in heating the oil to a conversion temperature in a heating zone, passing the oil to a conversion stage and there maintaining it in a substantial body, dephlegmating and condensing the evolved vapors and passing the uncondensed gases through an adsorbent substance. thereby adsorbing any vapors entrained by the uncondensed gases, driving off the adsorbed products by treating the adsorbent substance with'hea'ted gases of combustion from the heating zone so regulated as to relieve said substance of said products and condensing and collecting the products thus driven ofi.

2. A process for simultaneously cracking oil and recovering gasoline-like constituents from the uncondensed gases produced as a result of the cracking operation, consisting in subjecting the oil to cracking conditions of temperature and pressure, in dephlegmating' the evolved vapors, in subjecting the dephlegthese hydrocarbon a mated vapors to condensation, uncondensed gases through a bod of adsorbent substance, to adsorb gasoline- 'ke constituents entrained by the uncondensed gases, in

crackingprocess thereto, in regulating the admission of such heated combustion gases, so as to relieve said adsorbent substance of all of the adsorbed products, in thereafter condensing and collectin the products relieved from the adsorbent su stance.

3. A process for simultaneously cracking oil and recovering gasoline-like constituents from the uncondensed gases produced as a result of the cracking operation, consisting in subjecting the oil to cracking conditions of temperature and pressure, in dephlegmating the evolved vapors, in subjecting the dephlegmated vapors to condensation, in passing the uncondensed gases through a body of adsorbent substance, to adsorb gasoline-like constituents entrained by the uncondensed gases, in recovering the adsorbed gasoline like constituents from the adsorbentsubstance, by discontinuing the admission of uncondensed gases to such substance and admitting hot combustion gases from the heating zone of the cracking process thereto, in regulating the admission of such heated combustion gases, so as to relieve said adsorbent substance of all of the adsorbed products, in thereafter condensing and collecting the products relieved from the adsorbent substance, and in main- 4 taining a superatmospheric pressure upon the uncondensed gases passed through such ad sorbent substance.

4. A. process for simultaneously cracking oil and recovering gasoline-like constituents from the uncondensed gases produced as a result of the cracking operation, consisting in subjecting the oil to cracking conditions of temperature and pressure, in dephle ating the evolved vapors, in subjecting the ephlegmated vapors to condensation, in passing the unoondensed gases through a body of absorbent substance, to absorb gasoline-like constituents from the absorbent substance, b discontinuing the admission' of uncon ensed gases to such substance and raising the temperature of the body of absorbent material to relieve said absorbent substance of all absorbed products by waste heat from the heating zone of the cracking process, and condensing and collecting the products relieved from the absorbent substance.

GUSTAV EGLOFF. JACQUE O. MORRELL.

in passing the 

